U.S. patent number 4,003,826 [Application Number 05/626,151] was granted by the patent office on 1977-01-18 for hydrocarbon conversion with an acidic multimetallic catalytic composite.
This patent grant is currently assigned to UOP Inc.. Invention is credited to George J. Antos.
United States Patent |
4,003,826 |
Antos |
January 18, 1977 |
Hydrocarbon conversion with an acidic multimetallic catalytic
composite
Abstract
Hydrocarbons are converted by contacting them at hydrocarbon
conversion conditions with an acidic multimetallic catalytic
composite comprising a combination of catalytically effective
amounts of a platinum group component, a tin or lead component, a
lanthanide series component, and a halogen component with a porous
carrier material. The platinum group component, tin or lead
component, and halogen component are present in the multimetallic
catalyst in amounts respectively, calculated on an elemental basis,
corresponding to about 0.01 to about 2 wt. % platinum group metal,
about 0.01 to about 5 wt. % tin or lead, and about 0.1 to about 3.5
wt. % halogen. The lanthanide series component is present in
amounts corresponding to an atomic ratio of lanthanide series
component to platinum group metal of about 0.1:1 to about 1.25:1.
Moreover, these metallic components are uniformly dispersed
throughout the porous carrier material in carefully controlled
oxidation states such that substantially all of the platinum group
metal is present therein in the elemental metallic state, while
substantially all of the tin or lead component and of the
lanthanide series component are present therein in oxidation states
above that of the corresponding metal. A specific example of the
type of hydrocarbon conversion process disclosed in a process for
the catalytic reforming of a low-octane gasoline fraction wherein
the gasoline fraction and a hydrogen stream are contacted with the
novel acidic multimetallic catalyst disclosed herein at reforming
conditions.
Inventors: |
Antos; George J. (Arlington
Heights, IL) |
Assignee: |
UOP Inc. (Des Plaines,
IL)
|
Family
ID: |
27025606 |
Appl.
No.: |
05/626,151 |
Filed: |
October 28, 1975 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
Issue Date |
|
|
422464 |
Dec 6, 1973 |
3915845 |
|
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|
Current U.S.
Class: |
208/139 |
Current CPC
Class: |
B01J
23/622 (20130101); B01J 23/63 (20130101); C10G
35/09 (20130101); B01J 35/0093 (20130101); C07C
2521/04 (20130101); C07C 2523/02 (20130101); C07C
2523/04 (20130101); C07C 2523/10 (20130101); C07C
2523/14 (20130101); C07C 2523/42 (20130101); C07C
2523/44 (20130101); C07C 2523/46 (20130101); C07C
2523/62 (20130101) |
Current International
Class: |
B01J
23/62 (20060101); B01J 23/63 (20060101); B01J
23/54 (20060101); C10G 35/09 (20060101); C10G
35/00 (20060101); C10G 035/08 () |
Field of
Search: |
;208/139 ;252/466PT |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Davis; C.
Attorney, Agent or Firm: Hoatson, Jr.; James R. McBride;
Thomas K. Page, II; William H.
Parent Case Text
CROSS-REFERENCE TO RELATED APPLICATIONS
This application is a continuation-in-part of my prior copending
application Ser. No. 422,464 filed Dec. 6, 1973 now U.S. Pat. No.
3,915,845, issued Oct. 28, 1975. All of the teachings of this prior
application are specifically incorporated herein by reference.
Claims
I claim as my invention:
1. A process for converting a hydrocarbon which comprises
contacting the hydrocarbon at hydrocarbon conversion conditions
with an acidic catalytic composite comprising a porous carrier
material containing, on an elemental basis, about 0.01 to about 2
wt. % platinum group metal, about 0.01 to about 5 wt. % tin or
lead, about 0.1 to about 3.5 wt. % halogen, and a lanthanide series
component in an amount sufficient to result in an atomic ratio of
lanthanide series component to platinum group metal of about 0.1:1
to about 1.25:1, wherein the platinum group metal, tin or lead, and
lanthanide series component are uniformly dispersed throughout the
porous carrier material, wherein substantially all of the platinum
group metal is present in the elemental metallic state, wherein
substantially all of the tin or lead is present in an oxidation
state above that of the corresponding elemental metal, and wherein
substantially all of the lanthanide series component is present in
an oxidation state above that of the corresponding elemental
metal.
2. A process as defined in claim 1 wherein the platinum group metal
is platinum.
3. A process as defined in claim 1 wherein the platinum group metal
is palladium.
4. A process as defined in claim 1 wherein the platinum group metal
is iridium.
5. A process as defined in claim 1 wherein the halogen component is
combined chloride.
6. A process as defined in claim 1 wherein the porous carrier
material is a refractory inorganic oxide.
7. A process as defined in claim 6 wherein the refractory inorganic
oxide is alumina.
8. A process as defined in claim 1 wherein the lanthanide series
component is neodymium.
9. A process as defined in claim 1 wherein the lanthanide series
component is cerium.
10. A process as defined in claim 1 wherein the lanthanide series
component is lanthanum.
11. A process as defined in claim 1 wherein the lanthanide series
component is present in the catalytic composite in an amount
sufficient to result in an atomic ratio of lanthanide series
component to platinum group metal of about 0.4:1 to about 1:1.
12. A process as defined in claim 1 wherein substantially all of
the tin or lead is present in the catalytic composite as the
corresponding oxide.
13. A process as defined in claim 1 wherein substantially all of
the lanthanide series component is present in the catalytic
composite in the form of the corresponding oxide.
14. A process as defined in claim 1 wherein the atomic ratio of tin
or lead to platinum group metal contained in the composite is about
0.05:1 to about 10:1.
15. A process as defined in claim 1 wherein the catalytic composite
contains about 0.05 to about 1 wt.% platinum group metal, about
0.05 to about 2 wt.% tin or lead, 0.5 to about 1.5 wt.% halogen,
and an atomic ratio of lanthanide series component to platinum
group metal of about 0.4:1 to about 1:1.
16. A process as defined in claim 1 wherein the contacting of the
hydrocarbon with the catalytic composite is performed in the
presence of hydrogen.
17. A process as defined in claim 1 wherein the type of hydrocarbon
conversion is catalytic reforming of a gasoline fraction to produce
a high-octane reformate, wherein the hydrocarbon is contained in
the gasoline fraction, wherein the contacting is performed in the
presence of hydrogen and wherein the hydrocarbon conversion
conditions are reforming conditions.
18. A process as defined in claim 17 wherein the reforming
conditions include a temperature of about 800.degree. to
1100.degree. F., a pressure of about 0 to about 1000 psig., a
liquid hourly space velocity of about 0.1 to about 10
hr..sup..sup.-1, and a mole ratio of hydrogen to hydrocarbon of
about 1:1 to about 20:1.
19. A process as defined in claim 17 wherein the contacting step is
performed in a substantially water-free environment.
20. A process as defined in claim 17 wherein the reforming
conditions include a pressure of about 50 to about 350 psig.
Description
DISCLOSURE
The subject of the present invention is a novel acidic
multimetallic catalytic composite which has exceptional activity
and resistance to deactivation when employed in a hydrocarbon
conversion process that requires a catalyst having both a
hydrogenation-dehydrogenation function and a selective cracking
function. More precisely, the present invention involves a novel
dual-function acidic multimetallic catalytic composite which, quite
surprisingly, enables substantial improvements in hydrocarbon
conversion processes that have traditionally used a dual-function
catalyst. In another aspect, the present invention comprehends the
improved processes that are produced by the use of a catalytic
composite comprising a combination of catalytically effective
amounts of a platinum group component, a lanthanide series
component, a tin or lead component and a halogen component with a
porous carrier material; specifically, an improved reforming
process which utilizes the subject catalyst to improve activity,
selectivity, and stability characteristics.
Composites having a hydrogenation-dehydrogenation function and a
cracking function are widely used today as catalysts in many
industries, such as the petroleum and petrochemical industry, to
accelerate a wide spectrum of hydrocarbon conversion reactions.
Generally, the cracking function is thought to be associated with
an acid-acting material of the porpous, adsorptive, refractory
oxide type which is typically utilized as the support or carrier
for a heavy metal compound such as the transition metals or
compounds of the transition metals of Groups V through VIII of the
Periodic Table to which are generally attributed the
hydrogenation-dehydrogenation function.
These catalytic composites are used to accelerate a wide variety of
hydrocarbon conversion reactions such as hydrocracking,
isomerization, dehydrogenation, hydrogenation, desulfurization,
cyclization, alkylation, polymerization, cracking,
hydroisomerization, etc. In many cases, the commercial applications
of these catalysts are in processes where more than one of these
reactions are proceeding simultaneously. An example of this type of
process is reforming wherein a hydrocarbon feed stream containing
paraffins and naphthenes to aromatics, dehydrocyclization of
paraffins to aromatics, isomerization of paraffins and naphthenes,
hydrocracking of naphthenes and paraffins and the like reactions,
to produce an octane-rich or aromatic-rich product stream. Another
example is a hydrocracking process wherein catalysts of this type
are utilized to effect selective hydrogenation and cracking of high
molecular weight unsaturated materials, selective hydrocracking of
high molecular weight materials, and other like reactions, to
produce a generally lower boiling, more valuable output stream. Yet
another example is a hydroisomerization process wherein a
hydrocarbon fraction which is relatively rich in straight-chain
paraffins is contacted with a dual-function catalyst in the
presence of hydrogen to produce an output stream rich in
isoparaffins.
Regardless of the reaction involved or the particular process
involved, it is of critical importance that the dual-function
catalyst exhibit not only the capability to initially perform its
specified functions, but also that it has the capability to perform
them satisfactorily for prolonged periods of time. The analytical
terms used in the art to measure how well a particular catalyst
performs its intended functions in a particular hydrocarbon
reaction environment are activity, selectivity, and stability. And
for purposes of discussion here, these terms are conveniently
defined for a given charge stock as follows: (1) activity is a
measure of the catalyst's ability to convert hydrocarbon reactants
into products at a specified severity level where severity level
means the conditions used -- that is, the temperature, pressure,
contact time, and presence of diluents such as H.sub.2 ; (2)
selectivity refers to the amount of desired product or products
obtained relative to the amount of reactants charged or converted;
(3) stability refers to the rate of change with time of activity
and selectivity parameters -- obviously, the smaller rate implying
the more stable catalyst. In a reforming process, for example,
activity commonly refers to the amount of conversion that takes
place for a given charge stock at a specified severity level and is
typically measured by octane number of the C.sub.5 + product
stream; selectivity refers to the amount of C.sub.5 + yield,
relative to the amount of the charge, that is obtained at the
particular activity or severity level; and stability is typically
equated to the rate of change with time of activity, as measured by
octane number of C.sub.5 + product, and of selectivity, as measured
by C.sub.5 + yield. Actually, this last statement is not strictly
correct because generally a continuous reforming process is run to
produce a constant octane C.sub.5 + product with severity level
being continuously adjusted to attain this result; and,
furthermore, the severity level is for this purpose usually varied
by adjusting the conversion temperature in the reaction zone so
that, in point of fact, the rate of change activity finds response
in the rate of change of conversion temperature and changes in this
last parameter are customarily taken as indicative of activity
stability.
As is well known to those skilled in the art, the principal cause
of observed deactivation of instability of a dual-function catalyst
when it is used in a hydrocarbon conversion reaction is associated
with the fact that coke forms on the surface of the catalyst during
the course of the reaction. More specifically, in these hydrocarbon
conversion processes, the conditions utilized typically result in
the formation of heavy, high molecular weight, black, solid or
semi-solid, carbonaceous material which coats the surface of the
catalyst and reduces its activity by shielding its active sites
from the reactants. In other words the performance of this
dual-function catalyst is sensitive to the presence of carbonaceous
deposits on the surface of the catalyst. Accordingly, the major
problem facing workers in this area of the art is the development
of more active and selective catalytic composites that are not as
sensitive to the presence of these carbonaceous materials and/or
have the capability to suppress the rate of the formation of these
carbonaceous materials on the catalyst. Viewed in terms of
performance parameters, the problem is to develop a dual-function
catalyst having superior activity, selectivity, and stability. In
particular, for a reforming process the problem is typically
expressed in terms of shifting and stabalizing the C.sub.5 +
yield-octane relationship -- C.sub.5 + yield being representative
of selectivity and octane being proportional to activity.
I have now found a dual-function acidic multimetallic catalytic
composite which possesses improved activity, selectivity, and
stability characteristics when it is employed in a process for the
conversion of hydrocarbons of the type which have heretofore
utilized dual-function acidic catalytic composites such as
processes for isomerization, hydroisomerization, dehydrogenation,
desulfurization, denitrogenization, hydrogenation, alkylation,
dealkylation, hydrodealkylation, transalkylation, cyclization,
dehydrocyclization, cracking, hydrocracking, reforming,
disproportionation, polymerization, and the like processess. In
particular, I have ascertained that an acidic catalyst, comprising
a combination of catalytically effective amounts of a platinum
group component, a lanthanide series component, a tin or lead
component and a halogen component with a porous refractory carrier
material, can enable the performance of hydrocarbon conversion
processes utilizing dual-function catalysts to be substantially
improved if the metallic components are uniformly dispersed
throughout the carrier material in the hereinafter specified
amounts and if their oxidation states are controlled to be in the
states hereinafter specified. Moreover, I have determined that an
acidic catalytic composite, comprising a combination of
catalytically effective amounts of a platinum group component, a
lanthanide series component, a tin or lead component and a chloride
component with an alumina carrier material, can be utilized to
substantially improve the performance of a reforming process which
operates on a low-octane gasoline fraction to produce a
high-ocatane reformate if the metallic components are uniformly
distributed throughout the alumina carrier material in the proper
amounts and if their oxidation states are fixed in the states
hereinafter specified. In the case of a reforming process, the
principal advantage associated with the use of the novel catalyst
of the present invention involves the acquistion of the capability
to operate in a stable manner in a high severity operation; for
example, a low pressure reforming process designed to produce a
high yield of C.sub.5 + reformate having an ocatane of about 100
F-1 clear. As indicated, the present invention essentially involves
the finding that the addition of a tin or lead component and a
lanthanide series component to a dual-function acidic hydrocarbon
conversion catalyst containing a platinum group component can
enable the performance characteristics of the resulting catalyst to
be sharply and materially improved, if the hereinafter specified
limitations on amounts of ingredients, oxidation states of metals
and distribution of metallic components in the support are met.
It is, accordingly, one object of the present invention to provide
an acidic multimetallic hydrocarbon conversion catalyst having
superior preformance characteristics when utilized in a hydrocarbon
conversion process. A second object is to provide a multimetallic
catalyst having dual-function hydrocarbon conversion performance
characteristics that are relatively insensitive to the deposition
of hydrocarbonaceous material thereon. A third object is to provide
preferred methods of preparation of this catalytic composite which
insures the achievement and maintenance of its properties. Another
object is to provide an improved reforming catalyst having superior
activity, selectivity and stability characteristics. Yet another
object is to provide a dual-function hydrocarbon conversion
catalyst which utilizes a combination of a tin or lead component
and a lanthanide series component to promote an acidic catalyst
containing a platinum or palladium or iridium metal component.
In brief summary, the present invention is, in one embodiment, a
process for converting a hydrocarbon which comprises contacting the
hydrocarbon at hydrocarbon conversion conditions with an acidic
catalytic composite comprising a porous carrier material
containing, on an elemental basis, about 0.01 to about 2 wt. %
platinum group metal, about 0.1 to about 3.5 wt. % halogen, about
0.01 to about 5 wt. % tin or lead and a lanthanide series component
in an amount sufficient to result in an atomic ratio of lanthanide
series component to platinum group metal of about 0.1:1 to about
1.25:1, wherein the platinum group metal, lanthanide series
component and tin or lead are uniformly dispersed throughout the
porous carrier material, wherein substantially all of the platinum
group metal is present in the elemental metallic state and wherein
substantially all of the tin or lead and of the lanthanide series
component are present in an oxidation state above that of the
corresponding elemental metal.
A second embodiment involves a process for reforming a gasoline
fraction which comprises contacting the gasoline fraction, under
reforming conditions, with an acidic catalytic composite comprising
a porous carrier material containing, on an elemental basis, about
0.5 to about 1 wt. % platinum or palladium or iridium metal, about
0.5 to about 1.5 wt. % halogen, about 0.05 to about 2 wt. % tin or
lead, and a lanthanide series component in an amount sufficient to
result in an atomic ratio of lanthanide series component to
platinum or palladium or iriduim of about 0.4:1 to about 1:1,
wherein the platinum or palladium or iridium is present in the
corresponding elemental metallic state, wherein substantially all
of the tin or lead is present in an oxidation state above that of
the elemental metal and wherein substantially all of the lanthanide
series component is present in an oxidation state above that of the
corresponding elemental metal.
Other objects and embodiments of the present invention relate to
additional details regarding preferred catalytic ingredients,
preferred amounts of ingredients, suitable methods of composite
preparation, operating conditions for use in the hydrocarbon
conversion processes, and the like particulars which are
hereinafter given in the following detailed discussion of each of
these facets of the present invention.
The acidic multimetallic catalyst used in the process of the
present invention comprises a porous carrier material or support
having combined therewith catalytically effective amounts of a
platinum group component, a lanthanide series component, a Group
IVA metallic component, and a halogen component.
Considering first the porous carrier material utilized in the
present invention, it is preferred that the material be a porous,
adsorptive, high-surface area support having a surface area of
about 25 to about 500 m.sup.2 /g. The porous carrier material
should be relatively refractory to the conditions utilized in the
hydrocarbon conversion process, and it is intended to include
within the scope of the present invention carrier materials which
have traditionally been utilized in dual-function hydrocarbon
conversion catalysts such as: (1) activated carbon, coke, or
charcoal; (2) silica or silica gel, silicon carbide, clays and
silicates including those synthetically-prepared and
naturally-occuring, which may or may not be acid treated, for
example, attapulgus clay, china clay, diatomaceous earth, fuller's
earth, kaoline, kieselguhr, etc.; (3) ceramics, porcelain, crushed
firebrick, bauxite; (4) refractory inorganic oxides such as
alumina, titanium dioxide, zirconium dioxide, chromium oxide, zinc
oxide, magnesia, thoria, boria, silica-alumina, silica-magnesia,
chromia-alumina, alumina-boria, silica-zirconia, etc.; (5)
crystalline zeolitic aluminosilicates such as naturally-occuring or
synthetically-prepared mordenite and/or faujasite, either in the
hydrogen form or in a form which has been treated with multi-valent
cations; (6) spinels such as MgAl.sub. 2 O.sub.4, FeAl.sub. 2
O.sub.4, ZnAl.sub. 2 O.sub.4, CaAl.sub.2 O.sub.4 and other like
compounds have the formula MO.sup.. Al.sub. 2 O.sub.3 where M is a
metal havng a valence of 2, and (7) combinations of elements from
one or more of these groups. The preferred porous carrier materials
for use in the present invention are refractory inorganic oxides,
with best results obtained with an alumina carrier material.
Suitable alumina materials are the crystalline aluminas known as
the gamma-, eta-, and theta-alumina, with gamma- or eta- alumina
giving best results. In addition, in some embodiments the alumina
carrier material may contain minor proportions of other well known
refractory inorganic oxides such as silica, zirconia, magnesia,
etc.; however, the preferred support is substantially pure gamma-,
or eta-alumina. Preferred carrier materials have an apparent bulk
density of about 0.3 to about 0.7 g/cc and surface area
characteristics such that the average pore diameter is about 20 to
300 Angstroms, the pore volume is about 0.1 to about 1 cc/g and the
surface area is about 100 to about 500 m.sup.2 /g. In general, best
results are typically obtained with a gamma-alumina carrier
material which is used in the form of spherical particles having: a
relatively small diameter (i.e. typically about 1/16 inch), an
apparent bulk density of about 0.5 to about 0.6 g/cc, a pore volume
of about 0.4 cc/g, and a surface area of about 175 m.sup.2 /g.
The preferred alumina carrier material may be prepared in any
suitable manner and may be synthetically prepared or natural
occurring. Whatever type of alumina is employed it may be activated
prior to use by one or more treatments including drying
calcination, steaming, etc, and it may be in a form known as
activated alumina, activated alumina of commerce, porous alumina,
alumina gel, etc. For example, the alumina carrier may be prepared
by adding a suitable alkaline reagent, such as ammonium hydroxide
to a salt of aluminum such as aluminum chloride, aluminum nitrate,
etc., in an amount to form an aluminum hydroxide gel which upon
drying and calcining is converted to alumina. The alumina carrier
may be formed in any desired shape such as spheres, pills, cakes,
extrudates, powders, granules, tablets, etc., and utilized in any
desired size. For the purpose of the present invention a
particularly preferred form of alumina is the sphere; and alumina
spheres may be continuously manufactured by the well known oil drop
method which comprises: forming an alumina hydrosol by any of the
techniques taught in the art and preferably by reacting aluminum
metal with hydrochloric acid, combining the resulting hydrosol with
a suitable gelling agent and dropping the resultant mixture into an
oil bath maintained at elevated temperatures. The droplets of the
mixture remain in the oil bath until they set and form hydrogel
spheres. The spheres are then continuously withdrawn from the oil
bath and typically subjected to specific aging treatments in oil
and an ammoniacal solution to further improve their physical
characteristics. The resulting aged and gelled particles are then
washed and dried at a relatively low temperature of about
300.degree. F. to about 400.degree. F. and subjected to a
calcination procedure at a temperature of about 850.degree. F. to
about 1300.degree. F. for a period of about 1 to about 20 hours.
This treatment effects conversion of the alumina hydrogel to the
corresponding crystalline gamma-alumina. See the teachings of U.S.
Pat. No. 2,620,314 for additional details.
One essential constituent of the instant catalytic composite is the
tin or lead component. It is an essential feature of the present
invention that substantially all of the tin or lead component is
present in the final catalyst in an oxidation state above that of
the elemental metal. This component may be present in the catalytic
composite in chemical combination with one or more of the other
ingredients of the composite, or as a chemical compound of tin or
lead such as the corresponding oxide, sulfide, halide, oxyhalide,
oxychloride, aluminate, and the like compounds. Based on the
evidence currently available, it is believed that best results are
obtained when substantially all of the tin or lead component exists
in the final composite as tin oxide or lead oxide, respectively,
and the subsequently described oxidation and reduction steps, that
are used in the preparation of the instant composite, are believed
to result in an acidic multimetallic catalytic composite which
contains tin oxide or lead oxide. This component can be utilized in
the composite in any amount which is catalytically effective, with
the preferred amount being about 0.01 to about 5 wt. % thereof and
most especially about 0.05 to about 2 wt. % thereof, calculated on
an elemental basis. The exact amount selected within this broad
range is preferably determined as a function of the particular
metal that is utilized. For instance, in the case where this
component is lead, it is preferred to select the amount of this
component from the low end of this range -- namely about 0.01 to
about 1 wt. %. Additionally, it is preferred to select the amount
of lead as a function of the amount of the platinum group component
as explained hereinafter. In the case where this component is tin,
it is preferred to select from a relatively broader range of about
0.05 to about 2 wt. % thereof.
This tin or lead component may be incorporated in the composite in
any suitable manner known to the art to result in a uniform
dispersion of the metal moiety through out the carrier material
such as by coprecipitation or cogellation with the porous carrier
material, ion exchange with the carrier material, or impregnation
of the carrier material at any stage in its preparation. It is to
be noted that it is intended to include within the scope of the
present invention all conventional procedures for incorporating a
metallic component in a catalytic composite, and the particular
method of incorporation used is not deemed to be an essential
feature of the present invention so long as the tin or lead
component is relatively uniformly distributed throughout the porous
carrier material. One acceptable method of incorporating the tin or
lead component into the catalytic composite involves cogelling the
tin or lead component during the preparation of the preferred
carrier material, alumina. This method typically involves the
addition of a suitable soluble compound of tin or lead to the
alumina hydrosol. The resulting mixture is then commingled with a
suitable gelling agent, such as a relatively weak alkaline reagent,
and the resulting mixture is thereafter preferably gelled by
dropping into a hot oil bath as explained hereinbefore. After
aging, drying and calcining the resulting particles there is
obtained an intimate combination of the oxide of tin or lead and
alumina. One preferred method of incorporating this component into
the composite involves utilization of a soluble, decomposable
compound of tin or lead to impregnate the porous carrier material
either before, during or after the carrier material is calcined. In
general, the solvent used during this inpregnation step is selected
on the basis of its capability to dissolve the desired tin or lead
compound without affecting the porous carrier material which is to
be impregnated; ordinarily, good results are obtained when water is
the solvent; thus the preferred tin or lead compounds for use in
this impregnation step are typically water-soluble and
decomposable. Examples of suitable tin or lead compounds are:
stannous bromide, stannous chloride, stannic chloride, stannic
chloride diamine, stannic trichloride bromide, stannic chromate,
stannous fluoride, stannic iodide, stannic tartrate, lead acetate,
lead bromate, lead bromide, lead chlorate, lead chloride, lead
citrate, lead formate, lead lactate, lead malate, lead nitrate,
lead nitrite, lead ditnionate, and the like compounds. In the case
of tin, stannic or stannous chloride dissolved in water is
preferred. And in the case of lead, lead nitrate in water is
preferred. Regardless of which impregnation solution is utilized,
the tin or lead component can be impregnated either prior to,
simultaneously with, or after the other metallic components are
added to the carrier material. Ordinarily, best results are
obtained when this component is impregnated simultaneously with the
other metallic components of the composite. Likewise, best results
are ordinarily obtained when the tin or lead component is tin.
Regardless of which tin or lead compound is used in the preferred
impregnation step, it is important that the metal moiety be
uniformly distributed throughout the carrier material. In order to
achieve this objective it is necessary to maintain the pH of the
impregnation solution in a range of about 7 to about 1 or less and
to dilute the impregnation solution to a volume which is
approximately the same or greater than the volume of the carrier
material which is impregnated. Similarly, it is preferred to use a
relatively long contact time during the impregnation step ranging
from about 1/4 hour up to about 1/2 hour or more before drying to
remove excess solvent in order to insure a high dispersion of the
tin or lead component in the porous carrier material. The carrier
material is, likewise, preferably constantly agitated during this
preferred impregnation step.
A second essential ingredient of the subject catalyst is the
platinum group component. That is, it is intended to cover the use
of platinum or palladium or iridium or rhodium or osmium or
ruthenium or mixtures thereof as a second component of the present
composite. It is essential feature of the present invention that
substantially all of the platinum group component exists within the
final catalytic composite in the elemental metallic state (i.e. as
elemental platinum or palladium or iridium etc.). Generally the
amount of the second component used in the final composite is
relatively small compared to the amount of the other components
combined therewith. In fact, the platinum group component generally
will comprise about 0.01 to about 2 wt. % of the final catalytic
composite, calculated on an elemental basis. Excellent results are
obtained when the catalyst contains about 0.05 to about 1 wt. % of
platinum, iridium rhodium, or palladium metal. Particularly
preferred mixtures of these metals are platinum and iridium and
platinum and rhodium.
This platinum group component may be incorporated in the catalytic
composite in any suitable manner known to result in a relatively
uniform distribution of this component in the carrier material such
as coprecipitation or cogellation, ion-exchange, or impregnation.
The preferred method of preparing the catalyst involves the
utilization of a soluble, decomposable compound of a platinum group
metal to impregnate the carrier material in a relatively uniform
manner. For example, this component may be added to the support by
commingling the latter with an aqueous solution of chloroplatinic,
chloroiridic or chloropalladic acid. Other water-soluble compounds
of platinum group metals may be employed in impregnation solutions
and include ammonium chloroplatinate, bromoplatinic acid, platinum
dichloride, platinum tetrachloride hydrate, platinum
dichlorocarbonyl dichloride, dinitrodiaminoplatinum, tetramine
platinum chloride, palladium chloride, palladium nitrate, palladium
sulfate, etc. The utilization of a platinum group metal chloride
compound, such as chloroplatinic, chloroiridic or chloropalladic
acid, is preferred since it facilitates the incorporation of both
the platinum group component and at least a minor quantity of the
halogen component in a single step. Hydrogen chloride or the like
acid is also generally added to the impregnation solution in order
to further facilitate the incorporation of the halogen component
and the uniform distribution of the metallic component throughout
the carrier material. In addition, it is generally preferred to
impregnate the carrier material after it has been calcined in order
to minimize the risk of washing away the valuable platinum or
palladium compounds; however, in some cases it may be advantageous
to impregnate the carrier material when it is in a gelled
state.
Yet another essential of the present catalytic composite is a
lanthanide series component. By the use of the generic expression
"lanthanide series component" it is intended to cover the 15
elements and mixtures thereof that are commonly known as the
"lanthanide series" or "rare earths". Specifically, included within
this definition are the following elements: lanthanum, cerium,
praseodymium, neodymium, promethium, samarium, europium,
gadolinium, terbium, dysprosium, holmium, erbium, thulium,
ytterbium and lutetium. This component may be present in the
instant multimetallic composite in any form wherein substantially
all of the lanthanide element is present in an oxidation state
above that of the corresponding metal such as in chemical
combination with one or more of the other ingredients of the
composite, or as a chemical compound such as a lanthanide series
oxide, sulfide, halide, oxychloride, aluminate, and the like.
However, best results are believed to be obtained when
substantially all of the lanthanide series component exists in the
form of the corresponding oxide and the subsequently described
oxidation and prereduction procedure is believed, on the basis of
the available evidence, to result in this condition. This
lanthanide series component may be utilized in the composite in any
amount which is catalytically effective, with the preferred amount
being about 0.01 to about 1 wt. % thereof, calculated on an
elemental lanthanide basis. Typically best results are obtained
with about 0.05 to about 0.5 wt. % lanthanide element. According to
the present invention, it is essential to select the specific
amount of lanthanide series element from within this broad weight
range as a function of the amount of the platinum group component,
on an atomic basis, as is explained hereinafter. The lanthanie
series elements that are especially preferred for purposes of the
present invention are lanthanum, cerium, and neodymium, with
neodymium giving best results.
The lanthanide series component may be incorporated into the
catalytic composite in any suitable manner known to those skilled
in the catalyst formulation art which ultimately results in a
uniform dispersion of the lanthanide series moiety in the carrier
material. In addition, it may be added at any stage of the
preparation of the composite -- either during preparation of the
carrier material or thereafter -- and the precise method of
incorporation used is not deemed to be critical. However, best
results are obtained when the lanthanide series component is
incorporated in a manner such that it is relatively uniformly
distributed throughout the carrier material in a positive oxidation
state or a state which is easily converted to a positive oxidation
state in the subsequently described oxidation step. One preferred
procedure for incorporating this component into the composite
involves cogelling or coprecipitating the lanthanide series
component during the preparation of the preferred carrier material,
alumina. This procedure usually comprehends the addition of a
soluble, decomposable compound of a lanthanide series element such
as neodymium nitrate to the alumina hydrosol before it is gelled.
The resulting mixture is then finished by conventional gelling,
aging, drying and calcination steps as explained hereinbefore.
Another preferred way of incorporating this component is an
impregnation step wherein the porous carrier material is
impregnated with a suitable lanthanide series compound-containing
solution either before, during or after the carrier material is
calcined. Preferred impregnation solutions are aqueous solutions of
water-soluble, decomposable lanthanide series compounds such as a
lanthanide acetate, a lanthanide bromide, a lanthanide perchlorate,
a lanthanide chloride, a lanthanide iodide, a lanthanide nitrate,
and the like compounds. Best results are ordinarily obtained when
the impregnation solution is an aqueous solution of a lanthanide
chloride or a lanthanide nitrate. This lanthanide series component
can be added to the carrier material, either prior to,
simultaneously with, or after the other metallic components are
combined therewith. Best results are usually achieved when this
component is added simultaneously with the platinum group
component. In fact, excellent results have been obtained, as
reported in the examples, with a one step impregnation procedure of
a tin-containing aluminum carrier material using an aqueous
solution comprising the desired amounts of chloroplatinic acid, a
lanthanide nitrte, and hydrochloric acid.
It is essential to incorporate a halogen component into the
multimetallic catalytic composite of the present invention in an
amount sufficient to incorporate an acidic function therein.
although the precise form of the chemistry of the association of
the halogen component with the carrier material is not entirely
known, it is customary in the art to refer to the halogen component
as being combined with the carrier material, or with the other
ingredients of the catalyst in the form of the halide (e.g. as the
chloride). This combined halogen may be either fluorine, chlorine,
bromine, or mixtures thereof. Of these fluorine and, particularly,
chlorine are preferred for the purpose of the present invention.
The halogen may be added to the carrier material in any suitable
maner, either during preparation of the support or before or after
the addition of the other components. For example, the halogen may
be added, at any stage of the preparation of the carrier material
or to the calcined carrier material, as an aqueous solution of a
suitable, decomposable halogen-containing compound such as hydrogen
fluoride, hydrogen chloride, hydrogen bromide, ammonium chloride,
etc. The halogen component or a portion thereof, may be combined
with the carrier material during the impregnation of the latter
with the metallic components; for example, through the utilization
of a mixture of chloroplatinic acid and hydrogen chloride. In
another situation, the alumina hydrosol which is typically utilized
to form the preferred alumina carrier material may contain halogen
and thus contribute at least a portion of the halogen component to
the final composite. For reforming, the halogen will be typically
combined with the carrier material in an amount sufficient to
result in a final composite that contains about 0.1 to about 3.5%,
and preferably about 0.5 to about 1.5% by weight of halogen
calculated on an elemental basis. In isomerization or hydrocracking
embodiments, it is generally preferred to utilize relatively larger
amounts of halogen in the catalyst -- typically, ranging up to
about 10 wt. % halogen calculated on an elemental basis, and more
preferably about 1 to about 5 wt. %.
Regarding the preferred amounts of the various metallic components
of the subject catalyst, I have found it to be an essential
practice to specify the amounts of the lanthanide series component
as a function of the amount of the platinum group component. On
this basis, the amount of the lanthanide series component is
selected so that the atomic ratio of lanthanide series element to
the platinum group metal contained in the composite is about 0.1:1
to 1.25:1, with best results obtained when the range is about 0.4:1
to about 1:1. Similarly, it is a preferred practice to select the
amount of the tin or lead component to produce a composite
containing an atomic ratio of tin or lead to platinum group metal
within the broad range of about 0.05:1 to 10:1 However, for this
last parameter, the best practice is to select this ratio as
follows: (1) for tin, it is about 0.1:1 to 3:1, with the most
preferred range being about 0.5:1 to 1.5:1; and, (2) for lead, it
is about 0.05:1 to 0.9:1, with the most preferred range being about
0.1:1 to 0.75:1.
Another significant parameter for the present catalyst is the
"total metals content" which is defined to be the sum of the
platinum group component, the lanthanide series component, and the
tin or lead component, calculated on an elemental basis. Good
results are ordinarily obtained with the subject catalyst when this
parameter is fixed at a value of about 0.15 to about 2.5 wt. %,
with best results ordinarily achieved at a metals loading of about
0.3 to about 2 wt. %.
In embodiments of the present invention wherein the instant
multimetallic catalytic composite is used for dehydrogenation of
dehydrogenatable hydrocarbons or for the hydrogenation of
hydrogenatable hydrocarbons, it is ordinarily a preferred practice
to include an alkali or alkaline earth metal component in the
composite and to maintain the halogen component at the lowest
possible value. More precisely, this optional component is selected
from the group consisting of the compounds of the alkali metals --
cesium, rubidium, potassium, sodium and lithium -- and the
compounds of the alkaline earth metals -- calcium, strontium,
barium and magnesium. Generally, good results are obtained in these
embodiments when this component constitutes about 0.1 to about 5
wt. % of the composite, calculated on an elemental basis. This
optional alkali or alkaline earth metal component can be
incorporated in the composite in any of the known ways, with
impregnation with an aqueous solution of a suitable water-soluble,
decomposable compound being preferred.
An optional ingredient for the multimetallic catalyst of the
present invention is a Friedel-Crafts metal halide component. This
ingredient is particularly useful in hydrocarbon conversion
embodiments of the present invention wherein it is preferred that
the catalyst utilized has a strong acid or cracking function
associated therewith -- for example, an embodiment wherein
hydrocarbons are to be hydrocracked or isomerized with the catalyst
of the present invention. Suitable metal halides of the
Friedel-Crafts type include aluminum chloride, aluminum bromide,
ferric chloride, ferric bromide, zinc chloride, and the like
compounds, with the aluminum halides and particularly aluminum
chloride ordinarily yielding best results. Generally, this optional
ingredient can be incorporated into the composite of the present
invention by any of the conventional methods for adding metallic
halides of this type; however, best results are ordinarly obtained
when the metallic halide is sublimed onto the surface of the
carrier material according to the preferred method disclosed in
U.S. Pat. No. 2,999,074. The component can generally be utilized in
any amount which is catalytically effective, with a value selected
from the range of about 1 to about 100 wt. % of the carrier
material generally being preferred.
Regardless of the details of how the components of the catalyst are
combined with the porous carrier material, the final catalyst
generally will be dried at a temperature of about 200 to about
600.degree. F. for a period of at least about 2 to 24 hours or
more, and finally calcined or oxidized at a temperature of about
700.degree. F. to about 1100.degree. F. in an air atmosphere for a
period of about 0.5 to about 10 hours in order to convert
substantially all of the metallic components to the corresponding
oxide forms. Because a halogen component is utilized in the
catalyst, best results are generally obtained when the halogen
content of the catalyst is adjusted during the calcination step by
including a halogen or a halogen-containing compound in the air
atmosphere utilized. In particular, when the halogen component of
the catalyst is combined chloride, it is preferred to use a mole
ratio of H.sub.2 O to HC1 of about 5:1 to about 100:1 during at
least a portion of the calcination step in order to adjust the
final chlorine content of the catalyst to a range of about 0.1 to
about 3.5 wt. %.
It is an essential feature of the present invention that the
resultant oxidized trimetallic catalytic composite is subjected to
a substantially water-free reduction step prior to its use in the
conversion of hydrocarbons. This step is designed to insure a
uniform and finely divided dispersion of the metallic components
throughout the carrier material and to selectively reduce the
platinum group component to the corresponding metal while
maintaining substantially all of the tin or lead component and the
lanthanide series component in positive oxidation states.
Preferably, substantially pure and dry gydrogen (i.e. less than 20
vol. ppm. H.sub.2 O) is used as the reducing agent in this step.
The reducing agent is contacted with the oxidized catalyst at
conditions including a temperature of about 800.degree. F. to about
1200.degree. F. and a period of time of about 0.5 to 2 hours
effective to reduce sustantially all of the platinum group
component to the elemental metallic state while maintaining
substantially all of the tin or lead component and the lanthanide
series component in oxidation states above that of the
corresponding elemental metals. This reduction treatment may be
performed in situ as part of a start-up sequence if precautions are
taken to predry the plant to a substantially water-free state and
if substantially water-free hydrogen is used.
The resulting reduced catalytic composite may, in some cases, be
beneficially subjected to a presulfiding operation designed to
incorporate in the catalytic composite from about 0.05 to about 0.5
wt. % sulfur calculated on an elemental basis. Preferably, this
presulfiding treatment takes place in the presence of hydrogen and
a suitable sulfur-containing and metallic sulfide-producing
compound such as hydrogen sulfide, lower molecular weight
mercaptans, organic sulfides, disulfides, etc. Typically, this
procedure comprises treating the selectively reduced catalyst with
a sulfiding gas such as a mixture of hydrogen and hydrogen sulfide
having about 10 moles of hydrogen per mole of hydrogen sulfide at
conditions sufficient to effect the desired incorporation of
sulfur, generally including a temperature ranging from about
50.degree. F. up to about 1100.degree. F. or more. It is generally
a good practice to perform this presulfiding step under
substantially water-free conditions.
According to the present invention, a hydrocarbon charge stock and
hydrogen are contacted with the acidic multimetallic catalyst of
the present invention in a hydrocarbon conversion zone. This
contacting may be accomplished by using the catalyst in a fixed bed
system, a moving bed system, a fluidized bed system, or in a batch
type operation; however, a view of the danger of attrition losses
of the valuable catalyst and of well known operational advantages,
it is preferred to use a fixed bed system. In this system, a
hydrogen-rich gas and the charge stock are preheated by any
suitable heating means to the desired reaction temperature and then
are passed, into a conversion zone containing a fixed bed of the
catalyst type previously characterized. It is, of course,
understood that the conversion zone may be one or more separate
reactors with suitable means therebetween to insure that the
desired conversion temperature is maintained at the entrance to
each reactor. It is also important to note that the reactants may
be contacted with the catalyst bed in either upward, downward, or
radial flow fashion with the latter being preferred. In addition,
the reactants may be in the liquid phase, a mixed liquid-vapor
phase, or a vapor phase when they contact the catalyst, with best
results obtained in the vapor phase.
In the case where the multimetallic catalyst of the present
invention is used in a reforming operation, the reforming system
will comprise a reforming zone containing a fixed bed of the
catalyst type previously characterized. This reforming zone may be
one or more separate reactors with suitable heating means
therebetween to compensate for the endothermic nature of the
reactions that take place in each catalyst bed. The hydrocarbon
feed stream that is charged to this reforming system will comprise
hydrocarbon fractions containing naphthenes and paraffins that boil
within the gasoline range. The preferred charge stocks are those
consisting essentially of naphthenes and paraffins, although in
some cases aromatics and/or olefins may also be present. This
preferred class includes straight run gasolines, natural gasolines,
synthetc gasolines, partially reformed gasolines and the like. On
the other hand, it is frequently advantageous to charge thermally
or catalytically cracked gasolines or higher boiling fractions
thereof. Mixtures of straight run and cracked gasolines can also be
used to advantage. The gasoline charge stock may be a full boiling
gasoline having an initial boiling point of from about 50.degree.
F. to about 150.degree. F. and an end boiling point within the
range of from about 325.degree. F. to about 425.degree. F., or may
be a selected fraction thereof which generally will be a higher
boiling fraction commonly referred to as a heavy naphtha --for
example, a naphtha boiling in the range of C.sub.7 to 400.degree.
F. In some cases, it is also advantageous to charge pure
hydrocarbons or mixtures of hydrocarbons that have been extracted
from hydrocarbon distillates --for example, straight-chain
paraffins --which are to be converted to aromatics. It is preferred
that these charge stocks be treated by conventional catalytic
pretreatment methods such as hydrorefining, hydrotreating,
hydrodesulfurization, etc., to remove substantially all sulfurous,
nitrogenous and water-yielding contaminants therefrom and to
saturate any olefins that may be contained therein.
In other hydrocarbon conversion embodiments, the charge stock will
be of the conventional type customarily used for the particular
kind of hydrocarbon conversion being effected. For example, in a
typical isomerization embodiment the charge stock can be a
paraffinic stock rich in C.sub.4 to C.sub.8 normal paraffins, or a
normal butane-rich stock, or an n-hexane-rich stock, or a mixture
of xylene isomers, etc. In a dehydrogenation embodiment, the charge
stock can be any of the known dehydrogenatable hydrocarbons such as
an aliphatic compound containing 2 to 30 carbon atoms per molecule,
a C.sub.4 to C.sub.30 normal paraffin, a C.sub.8 to C.sub.12
alkylaromatic, a naphthene and the like. In hydrocracking
embodiments, the charge stock will be typically a gas oil, heavy
cracked cycle oil, etc. In addition alkylaromatic and naphthenes
can be conveniently isomerized by using the catalyst of the present
invention. Likewise, pure hydrocarbons or substantially pure
hydrocarbons can be converted to more valuable products by using
the trimetallic catalyst of the present invention in any of the
hydrocarbon conversion processes, known to the art, that use a
dual-function catalyst.
In a reforming embodiment, it is generally preferred to utilize the
novel multimetallic catalytic composite in a substantially
water-free environment. Essential to the achievement of this
condition in the reforming zone is the control of the water level
present in the charge stock and the hydrogen stream which is being
charged to the zone. Best results are ordinarily obtained when the
total amount of water entering the conversion zone from any source
is held to a level less than 50 ppm. and preferably less than 20
ppm.; expressed as weight of equivalent water in the charge stock.
In general, this can be accomplished by careful control of the
water present in the charge stock and in the hydrogen stream. The
charge stock can be dried by using any suitable drying means known
to the art such as a conventional solid adsorbent having a high
selectivity for water; for instance, sodium or calcium crystalline
aluminosilicates, silica gel, activated alumina, molecular sieves,
anhydrous calcium sulfate, high surface area sodium and the like
adsorbents. Similarly, the water content of the charge stock may be
adjusted by suitable stripping operations in a fractionation column
or like device. And in some cases, a combination of adsorbent
drying and distillation drying may be used advantageously to effect
almost complete removal of water from the charge stock. Preferably,
the charge stock is dried to a level corresponding to less than 20
ppm. of H.sub.2 O equivalent. In general, it is preferred to
maintain the hydrogen stream entering the hydrocarbon conversion
zone at a level of about 10 vol. ppm. of water or less. In the case
where the water content of hydrogen stream is above this range,
this can be conveniently accomplished by contacting the hydrogen
stream with a suitable desiccant such as those mentioned above at
conventional drying conditions.
In the reforming embodiment, an effluent stream is withdrawn from
the reforming zone and passed through a cooling means to a
separation zone, typically maintained at about 25.degree. to
150.degree. F., wherein a hydrogen-rich gas is separated from a
high octane liquid product, commonly called an "unstabilized
reformate". When a super-dry operation is desired, at least a
portion of this hydrogen-rich gas is withdrawn from the separating
zone and passed through an absorption zone containing an adsorbent
selective for water. The resultant substantially water-free
hydrogen stream can then be recycled through suitable compressing
means back to the reforming zone. The liquid phase from the
separating zone is typically withdrawn and commonly treated in a
fractionating system in order to adjust the butane concentration,
thereby controlling frontend volatility of the resulting
reformate.
The conditions utilized in the numerous hydrocarbon conversion
embodiments of the present invention are those customarily used in
the art for the particular reaction, or combination of reactions,
that is to be effected. For instance, alkylaromatics, olefin, and
paraffin isomerization conditions include: a temperature of about
32.degree. F. to about 1000.degree. F. and preferably about
75.degree. F. to about 600.degree. F.; a pressure of atomospheric
to about 100 atmospheres; a hydrogen to hydrocarbon mole ratio of
about 0.5:1 to about 20:1 and a LHSV (calculated on the basis of
equivalent liquid volume of the charge stock contacted with the
catalyst per hour divided by the volume of conversion zone
containing catalyst) of about 0.2 hr..sup. .sup.-1 to 10
hr..sup.116 1. Dehydrogenation conditions include: a temperature of
about 700.degree. to about 1250.degree. F., a pressure of about 0.1
to about 10 atmospheres, a liquid hourly space velocity of about 1
to 40 hr..sup..sup.-1 and a hydrogen to hydrocarbon mole ratio of
about 1:1 to 20:1. Likewise, typically hydrocracking conditions
include: a pressure of about 500 psig. to about 3000 psig.; a
temperature of about 400.degree. F. to about 900.degree. F.; a LHSV
of about 0.1 hr..sup..sup.-1 to about 10 hr..sup..sup.-1 ; and
hydrogen circulation rates of about 1000 to 10,000 SCF per barrel
of charge.
In the reforming embodiment of the present invention the pressure
utilized is selected from the range of about 0 psig. to about 1000
psig., with the preferred pressure being about 50 psig. to about
600 psig. Particularly good results are obtained at low pressure;
namely, a pressure of about 50 to 350 psig. In fact, it is a
singular advantage of the present invention that it allows stable
operation at lower pressure than have heretofore been successfully
utilized in so-called "continuous" reforming systems (i.e.
reforming for periods of about 15 to about 200 or more barrels of
charge per pound of catalyst without regeneration) with all
platinum monometallic catalysts. In other words, the multimetallic
catalyst of the present invention allows the operation of a
continuous reforming system to be conducted at low pressure (i.e.
100 to about 350 psig.) for about the same or better catalyst life
before regeneration as has been heretofore realized with
conventional monometallic catalysts at higher pressures (i.e. 400
to 600 psig.). On the other hand, the stability feature of the
present invention enables reforming operation conducted at
pressures of 400 to 600 psig. to achieve substantially increased
catalyst life before regeneration.
Similarly, the temperature required for reforming is generally
lower than that required for a similar reforming operation using a
high quality catalyst of the prior art. This significant and
desirable feature of the present invention is a consequence of the
selectivity of the acidic multimetallic catalyst of the present
invention for the octane-upgrading reactions that are preferably
induced in a typical reforming operation. Hence, the present
invention requires a temperature in the range of from about
800.degree. F. to about 1100.degree. F. and preferably about
900.degree. F. to about 1050.degree. F. As is well known to those
skilled in the continuous reforming art, the initial selection of
the temperature within this broad range is made primarily as a
function of the desired octane of the product reformate considering
the characteristics of the charge stock and of the catalyst.
Ordinarily, the temperature then is thereafter slowly increased
during the run to compensate for the inevitable deactivation that
occurs to provide a constant octane product. Therefore, it is a
feature of the present invention that the rate at which the
temperature is increased in order to maintain a constant octane
product, is substantially lower for the catalyst of the present
invention than for a high quality reforming catalyst which is
manufactured in exactly the same manner as the catalyst of the
present invention except for the inclusion of the lanthanide series
and tin or lead components. Moreover, for the catalyst of the
present invention, the C.sub.5 .sup.1/8 yield loss for a given
temperature increase is substantially lower than for a high quality
reforming catalyst of the prior art. In addition, hydrogen
production is substantially higher.
The reforming embodiment of the present invention also typically
utilizes sufficient hydrogen to provide an amount of about 1 to
about 20 moles of hydrogen per mole of hydrocarbon entering the
reforming zone, with excellent results being obtained when about 5
to about 10 moles of hydrogen are used per mole of hydrocarbon.
Likewise, the liquid hourly space velocity (LHSV) used in reforming
is selected from the range of about 0.1 to about 10
hr..sup..sup.-1, with a value in the range of about 1 to about 5
hr..sup..sup.-1 being preferred. In fact, it is a feature of the
present invention that it allows operations to be conducted at
higher LHSV than normally can be stably achieved in a continuous
reforming process with a high quality reforming catalyst of the
prior art. This last feature is of immense economic significance
because it allows a continuous reforming process to operate at the
same throughout level with less catalyst inventory than that
heretofore used with conventional reforming catalysts at no
sacrifice in catalyst life before regeneration.
The following examples are given to illustrate further the
preparation of the acidic multimetallic catalytic composite of the
present invention and the use thereof in the conversion of
hydrocarbons. It is understood that the examples are intended to be
illustrative rather than restrictive.
EXAMPLE I
A tin-containing alumina carrier material comprising 1/16 inch
spheres was prepared by: forming an aluminum hydroxyl chloride sol
by dissolving substantially pure aluminum pellets in a hydrochloric
acid solution, adding stannic chloride to the resulting sol in an
amount selected to result in a finished catalyst containing about
0.5 wt. % tin, adding hexamethylenetetramine to the resulting
tin-containing alumina sol, gelling the resulting solution by
dropping it into an oil bath to form spherical particles of an
aluminum- and tin-containing hydrogel, aging and washing the
resulting particles and finally drying and calcining the aged and
washed particles to form spherical particles of gamma-alumina
containing a uniform dispersion of about 0.5 wt. % tin in the form
of tin oxide and about 0.3 wt. % combined chloride. Additional
details as to this method of preparing the preferred gamma-alumina
carrier material are given in the teachings of U.S. Pat. No.
2,620,314.
An aqueous impregnation solution containing chloroplatinic acid,
neodymium nitrate and hydrogen chloride was then prepared. The
tin-containing alumina carrier material was thereafter admixed with
the impregnation solution. The amount of reagents contained in this
impregnation solution was calculated to result in a final composite
containing, on an elemental basis, 0.47 wt. % platinum, 0.26 wt. %
neodymium and 0.5 wt. % tin. In order to insure uniform dispersion
of the metallic components throughout the carrier material, the
amount of hydrochloric acid used was about 3 wt. % of the alumina
particles. This impregnation step was performed by adding the
carrier material particles to the impregnation mixture with
constant agitation. In addition, the volume of the solution was
approximately the same as the volume of the carrier material
particles. The impregnation mixture was maintained in contact with
the carrier material particles for a period of about 1/2 hour at a
temperature of about 70.degree. F. Thereafter, the temperature of
the impregnation mixture was raised to about 225.degree. F. and the
excess solution was evaporated in a period of about 1 hour. The
resulting dried particles were then subjected to a calcination or
oxidation treatment in an air atmosphere at a temperature of about
975.degree. F. for about 1 hour. This oxidation step was designed
to convert substantially all of the metallic ingredients to the
corresponding oxide forms. The calcined spheres were then contacted
with an air stream containing H.sub.2 O and HCl in a mole ratio of
about 30:1 for about 4 hours at 975.degree. F. in order to adjust
the halogen content of the catalyst particles to a value of about
1.05 wt. %.
The resulting catalyst particles were analyzed and found to
contain, on an elemental basis, about 0.47 wt. % platinum, about
0.26 wt. % neodymium, about 0.5 wt. % tin and about 1.05 wt. %
chloride. For this catalyst, the atomic ratio of tin to platinum is
1.75:1 and the atomic ratio of neodymium to platinum is 0.75:1.
Thereafter, the catalyst particles were subjected to a dry
pre-reduction treatment, designed to reduce the platinum component
to the elemental state while maintaining the tin and neodymium
components in positive oxidation states, by contacting them for 1
hour with a substantially pure hydrogen stream containing less than
5 vol. ppm. H.sub.2 O at a temperature of about 1050.degree. F., a
pressure slightly above atmospheric, and a flow rate of the
hydrogen stream through the catalyst particles corresponding to a
gas hourly space velocity of about 720 hr..sup..sup.-1. The
resulting catalyst is hereinafter referred to as catalyst "A".
EXAMPLE II
In order to compare the novel acidic multimetallic catalytic
composite of the present invention with a leading bimetallic
catalytic composite of the prior art in a manner calculated to
bring out the beneficial interaction between the lanthanide series
component and a platinum- and tin-containing catalyst, a comparison
test was made between the catalyst of the present invention, which
was prepared in Example I (i.e. catalyst A), and a superior
bimetallic reforming catalyst of the prior art which contained a
combination of platinum and tin as its
hydrogenation-dehydrogenation component. The control catalyst was a
combination of a platinum component, a tin component and a chloride
component with a gamma-alumina carrier material in an amount
sufficient to result in the final catalyst containing about 0.6 wt.
% platinum, about 0.5 wt. % tin and about 1.05 wt. % chloride. The
control catalyst is hereinafter referred to as catalyst "B".
Catalyst B was prepared by a method identical to that set forth in
Example I except for the inclusion of the lanthanide series element
and the increase in the platinum component from 0.47 wt. % to 0.6
wt. %.
These catalysts were then separately subjected to a high stress
accelerated catalytic reforming evaluation test designed to
determine in a relatively short period of time their relative
activity, selectivity and stability characteristics in a process
for reforming a relatively low-octane gasoline fraction. In both
tests the same charge stock was utilized and its pertinent
characteristics are set forth in Table I. It is to be noted that in
both cases the test was conducted under substantially water-free
conditions with the only significant source of water being the 5
wt. ppm. present in the charge stock. Likewise, it is to be
observed that both runs were performed under substantially
sulfur-free conditions with the only sulfur input into the plant
being the 0.1 wt. % sulfur contained in the charge stock.
TABLE I ______________________________________ Analysis of Charge
Stock Gravity, API at 60.degree. F. 60.3 Distillation Profile,
.degree. F. Initial Boiling Point 162 5% Boiling Point 186 10%
Boiling Point 200 30% Boiling Point 224 50% Boiling Point 252 70%
Boiling Point 286 90% Boiling Point 322 95% Boiling Point 338 End
Boiling Point 364 Chloride, wt. ppm. 0.1 Nitrogen, wt. ppm. 0.1
Sulfur, wt. ppm. 0.1 Water, wt. ppm. 5 Octane Number, F-1 Clear
43.8 Paraffins, vol. % 67.1 Naphthenes, vol. % 21.8 Aromatics, vol.
% 11.1 ______________________________________
This accelerated reforming test was specifically designed to
determine in a very short period of time whether the catalyst being
evaluated has superior characteristics for use in a high severity
reforming operation. Each run consisted of a series of evaluation
periods of 24 hours each, each of these periods comprised a 12 hour
line-out period followed by a 12 hour test period during which the
C.sub.5 + product reformate from the plant was collected and
analyzed. Both test runs were performed at identical conditions
which comprised a liquid hourly space velocity (LHSV) of 2.0
hr..sup..sup.-1, a pressure of 100 psig., a 5:1 gas to oil ratio,
and an inlet reactor temperature which was continuously adjusted
throughout the test in order to achieve and maintain a C.sub.5 +
target octane of 102 F-1 clear.
Both tests were performed in a pilot plant scale reforming unit
comprising a reactor containing the catalyst undergoing evaluation,
a hydrogen separation zone, a debutanizer column and suitable
heating means, pumping means, condensing means, compressing means
and the like conventional equipment. The flow scheme utilized in
this plant includes commingling a hydrogen recycle stream with the
charge stock and heating the resulting mixture to the desired
conversion temperature. The heated mixture is then passed downflow
into a reactor containing the catalyst undergoing evaluation as a
stationary bed. An effluent stream is then withdrawn from the
bottom of the reactor, cooled to about 70.degree. F. and passed to
a gas-liquid separation zone wherein a hydrogen-rich gaseous phase
separates from a liquid hydrocarbon phase. A portion of the gaseous
phase is then continuously passed through a high surface area
sodium scrubber and the resulting substantially water-free and
sulfur-free hydrogen stream is returned to the reactor in order to
supply the hydrogen recycle stream. The excess gaseous phase from
the separation zone is recovered as the hydrogencontaining product
stream (commonly called "excess recycle gas"). The liquid phase
from the separation zone is withdrawn therefrom and passed to a
debutanizer column wherein lightends (i.e. C.sub.1 to C.sub.4) are
taken overhead as debutanizer gas and a C.sub.5 + reformate stream
recovered as the principal bottom product.
The results of the separate test performed on the particularly
preferred catalyst of the present invention, Catalyst A, and the
control catalyst, Catalyst B, are presented for each test period in
Table II in terms of inlet temperature to the reactor in .degree.
F. necessary to achieve the target octane level, the amount of
C.sub.5 + reformate recovered expressed as vol. % of the charge
stock, and the purity of the recycle gas expressed as mole %
hydrogen contained in same. These results are shown in Table II as
a function of time expressed in barrels of charge processed per
pound of catalyst in the reactor (BPP).
TABLE II ______________________________________ Results of
Accelerated Reforming Test CATALYST "A" CATALYST "B" T, BPP T,
.degree. F C.sub.5 +, wt. % H.sub.2, % T, .degree. F C.sub.5 +,
wt.% H.sub.2,% ______________________________________ 0.4 968 77.4
86.0 967 77.0 86.4 0.6 971 77.8 86.7 975 77.0 86.7 0.8 978 -- 86.3
983 77.1 87.0 1.0 984 77.0 85.8 992 76.6 86.2 1.2 988 77.2 86.5 999
76.5 85.6 1.5 1004 -- 85.0 1013 76.0 84.0 1.7 1010 -- 84.3 -- -- --
______________________________________
Referring now to the results of the comparison test presented in
Table II, it is evident that the effect of the lanthanide series
component on the platinum and tin bimetallic catalyst is to
substantially promote same and to enable a catalyst containing less
platinum to outperform a catalyst containing a substantially
greater amount of platinum in the areas of activity, selectivity
and stability. That is, the data presented in Table II clearly
indicates that the catalyst of the present invention is markedly
superior to the control catalyst in a high severity reforming
process. As was pointed out in detail hereinbefore, a good measure
of activity for a reforming catalyst is the inlet temperature in
the reactor which is required to make target octane and the data
presented in Table II on this variable clearly shows that catalyst
A was significantly more active than catalyst B; for example, at a
time corresponding to 1.5 barrels of charge per pound of catalyst,
catalyst A required a reactor inlet temperature of 1004.degree. F.
in order to make octane which stands in sharp contrast to the
1013.degree. F. requirement of catalyst B at the same point in the
run. This 9.degree. F. difference in temperature requirement for
octane is conclusive evidence of the ability of the catalyst of the
present invention to materially accelerate the rate of the involved
reforming reaction in view of the well known rule of thumb that the
rate of reaction doubles with every 10.degree. C. change in reactor
temperature. Thus the data clearly shows that the composite of the
present invention was materially more active than the control
catalyst. However, activity is only one of the necessary
characteristics needed in order for a catalyst to demonstrate
superiority. Activity characteristics must be coupled with superior
selectivity and stability characteristics in order to demonstrate
improved performance. Selectivity is measured directly by C.sub.5 +
yield and the data presented in Table II clearly indicates that
catalyst A consistently produced better yields than catalyst B. (It
is to be noted that the dashes in Table II represent periods where
the relevant analyses of the product streams were not made.)
Another indication of good selectivity characteristics is the
hydrogen content of the excess recycle gas and on this basis the
catalyst of the present invention exhibited hydrogen purity which
was analogous to that observed for catalyst B. On the other hand,
good stability characteristics are shown by the rate of change of
the activity and selectivity parameters as was explained
hereinbefore, and on the basis the incremental change in
temperature required to maintain octane and in C.sub.5 + yield
exhibited in Table II clearly shows superior stability for the
catalyst of the present invention.
In summary, it is clear from the data presented in Table II that a
lanthanide series element, neodymium, is an efficient and effective
promoter for a platinum- and tin-containing reforming catalyst in a
high severity reforming operation.
It is intended to cover by the following claims, all changes and
modifications of the above disclosure of the present invention
which would be self-evident to a man of ordinary skill in the
hydrocarbon conversion art or the catalyst formulation art.
* * * * *